CN101279891A - Method for purification of glycerol - Google Patents
Method for purification of glycerol Download PDFInfo
- Publication number
- CN101279891A CN101279891A CNA2007103005238A CN200710300523A CN101279891A CN 101279891 A CN101279891 A CN 101279891A CN A2007103005238 A CNA2007103005238 A CN A2007103005238A CN 200710300523 A CN200710300523 A CN 200710300523A CN 101279891 A CN101279891 A CN 101279891A
- Authority
- CN
- China
- Prior art keywords
- glycerine
- resin
- bed
- weight
- raw glycerine
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 title claims abstract description 101
- 238000000034 method Methods 0.000 title claims abstract description 24
- 238000000746 purification Methods 0.000 title abstract description 7
- 239000011324 bead Substances 0.000 claims abstract description 12
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000003456 ion exchange resin Substances 0.000 claims abstract description 9
- 229920003303 ion-exchange polymer Polymers 0.000 claims abstract description 9
- 239000003225 biodiesel Substances 0.000 claims abstract description 6
- 230000002378 acidificating effect Effects 0.000 claims abstract description 5
- 238000004519 manufacturing process Methods 0.000 claims abstract description 5
- 235000011187 glycerol Nutrition 0.000 claims description 41
- 239000011347 resin Substances 0.000 claims description 24
- 229920005989 resin Polymers 0.000 claims description 24
- 239000003795 chemical substances by application Substances 0.000 claims description 9
- 150000001768 cations Chemical class 0.000 claims description 4
- 239000006227 byproduct Substances 0.000 claims description 2
- 239000003054 catalyst Substances 0.000 claims description 2
- 239000002245 particle Substances 0.000 claims description 2
- 150000003839 salts Chemical class 0.000 abstract description 3
- -1 fatty acid salts Chemical class 0.000 abstract description 2
- 235000014113 dietary fatty acids Nutrition 0.000 abstract 1
- 229930195729 fatty acid Natural products 0.000 abstract 1
- 239000000194 fatty acid Substances 0.000 abstract 1
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 9
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 239000002253 acid Substances 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 239000000446 fuel Substances 0.000 description 5
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 4
- 239000000344 soap Substances 0.000 description 4
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 3
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 229910017053 inorganic salt Inorganic materials 0.000 description 3
- 150000002632 lipids Chemical class 0.000 description 3
- 229910052708 sodium Inorganic materials 0.000 description 3
- 239000011734 sodium Substances 0.000 description 3
- 241000209094 Oryza Species 0.000 description 2
- 235000007164 Oryza sativa Nutrition 0.000 description 2
- 239000002551 biofuel Substances 0.000 description 2
- 150000001721 carbon Chemical group 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 125000000524 functional group Chemical group 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 229910052700 potassium Inorganic materials 0.000 description 2
- 239000011591 potassium Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 235000009566 rice Nutrition 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000005809 transesterification reaction Methods 0.000 description 2
- HIXDQWDOVZUNNA-UHFFFAOYSA-N 2-(3,4-dimethoxyphenyl)-5-hydroxy-7-methoxychromen-4-one Chemical compound C=1C(OC)=CC(O)=C(C(C=2)=O)C=1OC=2C1=CC=C(OC)C(OC)=C1 HIXDQWDOVZUNNA-UHFFFAOYSA-N 0.000 description 1
- 239000004925 Acrylic resin Substances 0.000 description 1
- 229920000178 Acrylic resin Polymers 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- BAPJBEWLBFYGME-UHFFFAOYSA-N Methyl acrylate Chemical compound COC(=O)C=C BAPJBEWLBFYGME-UHFFFAOYSA-N 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- QYKIQEUNHZKYBP-UHFFFAOYSA-N Vinyl ether Chemical compound C=COC=C QYKIQEUNHZKYBP-UHFFFAOYSA-N 0.000 description 1
- DPDMMXDBJGCCQC-UHFFFAOYSA-N [Na].[Cl] Chemical compound [Na].[Cl] DPDMMXDBJGCCQC-UHFFFAOYSA-N 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- XZKRXPZXQLARHH-UHFFFAOYSA-N buta-1,3-dienylbenzene Chemical group C=CC=CC1=CC=CC=C1 XZKRXPZXQLARHH-UHFFFAOYSA-N 0.000 description 1
- 150000001732 carboxylic acid derivatives Chemical class 0.000 description 1
- 125000002843 carboxylic acid group Chemical group 0.000 description 1
- 239000003729 cation exchange resin Substances 0.000 description 1
- 235000013339 cereals Nutrition 0.000 description 1
- 229920001577 copolymer Polymers 0.000 description 1
- 238000004132 cross linking Methods 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 239000008367 deionised water Substances 0.000 description 1
- 229910021641 deionized water Inorganic materials 0.000 description 1
- POLCUAVZOMRGSN-UHFFFAOYSA-N dipropyl ether Chemical compound CCCOCCC POLCUAVZOMRGSN-UHFFFAOYSA-N 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- RTZKZFJDLAIYFH-UHFFFAOYSA-N ether Substances CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 1
- 150000002334 glycols Chemical class 0.000 description 1
- 238000001032 ion-exclusion chromatography Methods 0.000 description 1
- 150000002605 large molecules Chemical class 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 150000004702 methyl esters Chemical class 0.000 description 1
- 230000003278 mimic effect Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- YPHQUSNPXDGUHL-UHFFFAOYSA-N n-methylprop-2-enamide Chemical compound CNC(=O)C=C YPHQUSNPXDGUHL-UHFFFAOYSA-N 0.000 description 1
- 230000002572 peristaltic effect Effects 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 239000000049 pigment Substances 0.000 description 1
- 229920005862 polyol Polymers 0.000 description 1
- 150000003077 polyols Chemical class 0.000 description 1
- 229920001289 polyvinyl ether Polymers 0.000 description 1
- 239000001103 potassium chloride Substances 0.000 description 1
- 235000011164 potassium chloride Nutrition 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000012508 resin bead Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 159000000000 sodium salts Chemical group 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 235000020354 squash Nutrition 0.000 description 1
- UFTFJSFQGQCHQW-UHFFFAOYSA-N triformin Chemical compound O=COCC(OC=O)COC=O UFTFJSFQGQCHQW-UHFFFAOYSA-N 0.000 description 1
- 235000013311 vegetables Nutrition 0.000 description 1
- KAKZBPTYRLMSJV-UHFFFAOYSA-N vinyl-ethylene Natural products C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A method for purification of glycerol, especially crude glycerol from biodiesel production. The method uses gel-type acidic ion exchange resin beads to separate fatty acid salts and inorganic salts from the crude glycerol.
Description
Technical field
The present invention relates to the glycerin purification method, be specifically related to be derived from the purification process of the raw glycerine that biofuel (biodiesel) produces.
Background technology
High fuel price and environmental problem are promoting people and are developing alternative fuel, particularly are derived from the fuel of renewable resources.A kind of such fuel is commonly called " biofuel " fuel, comprises the methyl esters of lipid acid usually, burns in diesel engine.A transesterification reaction that the source is a tri-glyceride of biodiesel fuel, for example transesterification reaction of vegetables oil and alcohol (normally methyl alcohol).Glycerine makes as the by product of this technology, contains soap and inorganic salt pollutent usually.Prior art has disclosed the method for glycerine being carried out purifying, and for example D.R.Asher and D.W.Simpson are at J.Phys.Chem., and the 60th rolls up, and the ion exclusion chromatography of passing through that discloses in the 518-21 page or leaf (1956) is carried out glycerin purification.But the separation that method of the prior art realizes is relatively poor.
Problem solved by the invention is to find a kind of improved method that is used for glycerine is carried out purifying.
Summary of the invention
The present invention relates to a kind of method of glycerine being carried out purifying.This method may further comprise the steps: the catalyst beads that comprises the gel-type acidic ion exchange resin (a) is provided, and described bead has: (i) be not more than 1.15 uniformity ratio; The (ii) monomeric unit that is derived from linking agent of 4-8 weight %; The (iii) harmonic mean granularity of 200-400 micron; (b) make the bed that passes through described bead from the raw glycerine of production of biodiesel.
Embodiment
Unless otherwise indicated, all percentage ratio is weight percentage (" weight % "), and all temperature units are ℃.Weight percentage about ion exchange resin is to be benchmark in the dried resin.Lipid acid is the no cycloaliphatic carboxylic acid who comprises 8-22 carbon atom; Most preferably it comprises 12-18 carbon atom.About C-C, described lipid acid can be saturated, monounsaturated or polyunsaturated (comprising two or three carbon-to-carbon double bonds usually).
Except glycerine, comprise methyl alcohol, water, inorganic salt and soap usually from the raw glycerine of production of biodiesel.Salt is sodium salt and/or sylvite normally.The content of soap is generally 5-50%.The content of inorganic salt is 1-5%.These content common one are reinstated total cation concentration and are represented; Its concentration is generally 0.2-5%.In some embodiments of the present invention, described total cation concentration is at least 0.5%, perhaps is at least 1%.In some embodiments, described total cation concentration is not more than 4%, perhaps is not more than 3%.Raw glycerine comprises water, goes back dilutable water, reducing the load of coupled columns (column), and helps to separate, and therefore water-content can be 5-40% usually.In some embodiments of the present invention, the glycerol concentration of introducing the raw glycerine in the resin bed is at least 20%, perhaps is at least 30%, perhaps is at least 40%, perhaps is at least 50%, perhaps is at least 60%, perhaps is at least 70%, perhaps is at least 75%.Method of the present invention also can be used to the raw glycerine available from other source (comprising the soap manufacturing) is carried out purifying.
In some embodiments of the present invention, the purifying of described glycerine carries out under 25-80 ℃ temperature.In some embodiments of the present invention, described temperature is not higher than 70 ℃, perhaps is not higher than 65 ℃, perhaps is not higher than 60 ℃.In some embodiments of the present invention, described temperature is at least 40 ℃, perhaps is at least 45 ℃.Higher temperature can be improved separation usually, but even the present invention in the temperature lower than the temperature of common employing and under than the higher concentration of the glycerol concentration that adopts usually, also can provide improved separating effect.
According to the present invention, be used for the isolating conventional flow velocity of glycerine and be 0.2-1 bed volume (" BV ")/hour.In some embodiments of the present invention, described flow velocity was at least 0.3BV/ hour, perhaps was at least 0.4BV/ hour.In some embodiments of the present invention, described flow velocity is not more than 0.9BV/ hour, perhaps is not more than 0.8BV/ hour.
Being used for ion exchange resin of the present invention is gel type resin, rather than macroreticular resin.Macroreticular resin is that surface-area is a 25-200 rice
2/ gram, mean pore size are
Resin; Or surface-area is a 30-80 rice
2/ gram, mean pore size are
Resin.The gel-like resin comprises usually and is not more than 10% the monomeric unit that is derived from linking agent.Suitable gel-like resin comprises for example acrylic resin, styrene resin, and their combination.Resin comprises the polymerized unit of multi-ethylenical unsaturated monomer (linking agent).In some embodiments of the present invention, the content that is derived from the monomeric unit of linking agent in the resin is not more than 7.5%, perhaps is not more than 7%, perhaps is not more than 6.5%, perhaps is not more than 6%.In some embodiments, the content of described linking agent is at least 4.5%.In some embodiments, the mean particle size of described gel resin is the 250-400 micron, perhaps is the 250-350 micron.In some embodiments of the present invention, described ion exchange resin comprises the polymerized unit of vinylbenzene and linking agent, for example divinyl aromatic compound; Two, three and four (methyl) acrylate or (methyl) acrylamide; Two-, three-and tetraallyl ether and ester; The polyenoid propyl ether of two pure and mild polyvalent alcohols and many vinyl ether (polyallyl and polyvinyl ethers of glycols and polyols).In following embodiment of the present invention, described linking agent is that two ethylenic are undersaturated, for example is Vinylstyrene (DVB).In some embodiments of the present invention, the acid functional group of described ion exchange resin comprises sulfonic group, carboxylic acid group, phosphate or its mixture.Conventional acidic ion exchange resin is that the acid functionality of benchmark is 0.4-8 milliequivalent/kilogram in the dry weight, perhaps is at least 2 milliequivalent/kilograms, perhaps is at least 4 milliequivalent/kilograms.Preferably, described acid functional group is sulfonic form.It is believed that with the positively charged ion of resin-bonded unimportant, but according to positively charged ion main in the raw glycerine, be generally sodium or potassium.
The uniformity ratio of ion-exchange resin bead grain size-grade distribution is the tolerance of size distribution curve width.Described uniformity ratio is defined as d60/d10, and wherein d60 is the size of the opening (opening) that lucky 60% bead can pass through in distributing, and d10 is the size of the opening that lucky 10% bead can pass through in distributing.In some embodiments of the present invention, the uniformity ratio of described resin beads is not more than 1.10.
In the method for the invention, than glycerine wash-out from pillar earlier, the glycerine that makes has much lower metal ion content and the color that weakens greatly usually for salt and foreign pigment.
Method of the present invention can be used mimic moving bed technique or successive simulated moving bed technology, to realize the automatization continuous purification to glycerine.
Embodiment
Embodiment 1
To there be the chromatographic column (2 meters of internal diameter 1.5 cm x) of chuck to be heated to 60 ℃.Keep temperature by making water cross described chuck from the water bath with thermostatic control cycling stream.Described chromatographic column is filled to 194 with the potassium form of acidic cation-exchange resin bead, the height of 6 centimetres (345 milliliters), described bead are by sulfonated phenylethylene/DVB copolymer, and the harmonic mean granularity is 300 microns, crosslinking degree is 5%, and uniformity ratio is not more than 1.15.Described resin bed is fixed, and makes the resin bed temperature reach balance before operation.Feedstock solution is by pure glycerin solution and Repone K preparation, and glycerol concentration is 68%, and potassium content is 4.2%, and the pH value is 5-9.At buried resin bed higher slice (layered),, make described feedstock solution pass through resin bed the feedstock solution of the amount of recording with the flow velocity (3 ml/min) of control by regulating the rotating speed of peristaltic pump.Use deionized water as eluting solvent.Detect meter successive analysis effluent by differential refractometer.Use the signal response of conductometer detector check Repone K.Find that differential refractometer detects the concentration that meter can be used for analyzing glycerine and Repone K.Inject the suitability that Repone K comes checking system after injecting some glycerine solutions.All parameters are measured with the independent color atlas of Repone K and glycerine solution.In order to check the separating property of resin, inject the resulting solution of glycerine and Repone K.
For the difference that will cause owing to the bed size of input concentration minimizes, with the overhead product volume divided by the resin bed volume, with the overhead product concentration of glycerine and Repone K respectively divided by the concentration of glycerine in the feedstock solution and Repone K.
The porosity of resin bed is measured by injecting very large molecule (making molecule can not be held).By measuring the retention time of the described molecule that does not keep, the bed porosity directly provides with bed volume.This parameter has shown the balance that resin bed is filled.
Embodiment 2
The solution that will comprise sodium-chlor and glycerine (glycerol concentration is 68%, and sodium content is 4.5%) is annotated on the sodium type according to the resin of the step of embodiment 1.
Isolating parameter is listed in the table below:
Claims (9)
1. method of glycerine being carried out purifying.This method may further comprise the steps:
(a) provide the catalyst beads that comprises the gel-type acidic ion exchange resin, described bead has: (i) be not more than 1.15 uniformity ratio; The (ii) monomeric unit that is derived from linking agent of 4-8 weight %; The (iii) harmonic mean granularity of 200-400 micron;
(b) make the bed of described raw glycerine by described bead.
2. the method for claim 1 is characterized in that, the glycerol concentration in the described raw glycerine is at least 40 weight %.
3. method as claimed in claim 2 is characterized in that, described resin comprises the monomeric unit that is derived from linking agent of 4-6.5 weight %.
4. method as claimed in claim 3 is characterized in that, described raw glycerine with at least 0.3 bed volume/hour flow velocity by described bed.
5. method as claimed in claim 4 is characterized in that, the mean particle size of described resin is the 250-400 micron.
6. method as claimed in claim 5 is characterized in that, described raw glycerine is the by product of production of biodiesel.
7. method as claimed in claim 6 is characterized in that, total cation concentration is at least 1 weight % in the described raw glycerine
8. method as claimed in claim 7 is characterized in that, the glycerol concentration in the described raw glycerine is at least 60 weight %.
9. method as claimed in claim 8 is characterized in that, the temperature of described bed remains on and is not higher than 70 ℃.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP07290412.1 | 2007-04-04 | ||
| EP07290412 | 2007-04-04 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101279891A true CN101279891A (en) | 2008-10-08 |
| CN101279891B CN101279891B (en) | 2011-08-10 |
Family
ID=38372417
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2007103005238A Expired - Fee Related CN101279891B (en) | 2007-04-04 | 2007-12-20 | Method for purification of glycerol |
Country Status (4)
| Country | Link |
|---|---|
| US (1) | US7667081B2 (en) |
| EP (1) | EP1978009A1 (en) |
| CN (1) | CN101279891B (en) |
| BR (1) | BRPI0704952A2 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102229521A (en) * | 2011-05-14 | 2011-11-02 | 江门市鸿捷精细化工有限公司 | Process for refining crude glycerin and recovering byproducts |
| CN102391069A (en) * | 2011-09-05 | 2012-03-28 | 德源(中国)高科有限公司 | Preparation method of high-purity glycerol |
| CN101759526B (en) * | 2010-01-13 | 2012-07-18 | 湖南省林业科学院 | Refining production method of glycerin |
| CN104603238A (en) * | 2012-08-29 | 2015-05-06 | 阿彻丹尼尔斯米德兰德公司 | Removal of organic salts from bio-derived glycol products |
Families Citing this family (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7534923B2 (en) * | 2007-08-15 | 2009-05-19 | Rohm And Haas Company | Method for purification of glycerol from biodiesel production |
| WO2009099804A2 (en) * | 2008-02-01 | 2009-08-13 | Lanxess Sybron Chemicals Inc. | A process for the purification of crude glycerin utilizing ion exclusion chromatorgraphy and glycerin concentration |
| US8470078B2 (en) * | 2008-03-12 | 2013-06-25 | Ihi E&C International Corporation | Process for removing tar from synthesis gas |
| FR2938535B1 (en) | 2008-11-20 | 2012-08-17 | Arkema France | PROCESS FOR PRODUCING METHYLMERCAPTOPROPIONALDEHYDE AND METHIONINE FROM RENEWABLE MATERIALS |
| JP5595719B2 (en) | 2008-12-25 | 2014-09-24 | 花王株式会社 | Method for producing glycerin |
| US20110004031A1 (en) * | 2009-05-06 | 2011-01-06 | S.I.I., Llc | Glycerin purification |
| US8022257B2 (en) * | 2009-09-03 | 2011-09-20 | The Ohio State University Research Foundation | Methods for producing polyols using crude glycerin |
| EP2295394A1 (en) | 2009-09-11 | 2011-03-16 | Rhodia Poliamida E Especialidades Ltda | Process for the purification of crude glycerol |
| FR2953829B1 (en) | 2009-12-14 | 2011-12-09 | Arkema France | PROCESS FOR PRODUCING ACROLEIN AND / OR ACRYLIC ACID FROM GLYCEROL |
| FR2953830B1 (en) | 2009-12-14 | 2012-01-20 | Arkema France | PROCESS FOR PRODUCING ACROLEIN AND / OR ACRYLIC ACID FROM GLYCEROL |
| US8759595B2 (en) | 2011-10-12 | 2014-06-24 | Vertichem Corporation | Method of biobased chemical production from crude bioglycerin |
| KR20190017074A (en) | 2013-08-19 | 2019-02-19 | 알이지 라이프 사이언시스, 엘엘씨 | Production of partially refined waste glycerol |
| US9469586B2 (en) | 2013-08-19 | 2016-10-18 | REG Life Sciences, LLC | Production of partially refined waste glycerol |
| FR3017617B1 (en) | 2014-02-19 | 2016-02-12 | Arkema France | PROCESS FOR PRODUCING BIO-SOURCE ACRYLIC ACID |
| CN105418378A (en) * | 2015-11-27 | 2016-03-23 | 宁波滨海石化有限公司 | Purification technology of ester exchange by-product glycerol |
| WO2017119007A1 (en) | 2016-01-07 | 2017-07-13 | Institute Of Chemical Technology | Process for purification and refining of glycerol |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB633343A (en) * | 1945-09-15 | 1949-12-12 | American Cyanamid Co | Improvements in or relating to process of purifying glycerine containing ionizable impurities |
| US2615924A (en) * | 1950-08-31 | 1952-10-28 | Illinois Water Treat Co | Method of purifying glycerin |
| JPS58144333A (en) * | 1982-02-20 | 1983-08-27 | Nippon Oil & Fats Co Ltd | Glycerin purification method |
| CA1329782C (en) | 1988-08-09 | 1994-05-24 | Thomas Buenemann | Process for purifying crude glycerol |
| US7126032B1 (en) | 2006-03-23 | 2006-10-24 | Sunoco, Inc. (R&M) | Purification of glycerin |
-
2007
- 2007-12-14 BR BRPI0704952-8A patent/BRPI0704952A2/en not_active IP Right Cessation
- 2007-12-14 EP EP07254866A patent/EP1978009A1/en not_active Withdrawn
- 2007-12-20 CN CN2007103005238A patent/CN101279891B/en not_active Expired - Fee Related
- 2007-12-21 US US12/004,547 patent/US7667081B2/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101759526B (en) * | 2010-01-13 | 2012-07-18 | 湖南省林业科学院 | Refining production method of glycerin |
| CN102229521A (en) * | 2011-05-14 | 2011-11-02 | 江门市鸿捷精细化工有限公司 | Process for refining crude glycerin and recovering byproducts |
| CN102229521B (en) * | 2011-05-14 | 2013-11-06 | 江门市鸿捷精细化工有限公司 | Process for refining crude glycerin and recovering byproducts |
| CN102391069A (en) * | 2011-09-05 | 2012-03-28 | 德源(中国)高科有限公司 | Preparation method of high-purity glycerol |
| CN104603238A (en) * | 2012-08-29 | 2015-05-06 | 阿彻丹尼尔斯米德兰德公司 | Removal of organic salts from bio-derived glycol products |
Also Published As
| Publication number | Publication date |
|---|---|
| EP1978009A1 (en) | 2008-10-08 |
| CN101279891B (en) | 2011-08-10 |
| US20080249338A1 (en) | 2008-10-09 |
| BRPI0704952A2 (en) | 2008-11-18 |
| US7667081B2 (en) | 2010-02-23 |
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